CN101486625A - Fractionation process for cracking gas from oxidation pyrolysis of gaseous hydrocarbon - Google Patents
Fractionation process for cracking gas from oxidation pyrolysis of gaseous hydrocarbon Download PDFInfo
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- CN101486625A CN101486625A CNA2009100091230A CN200910009123A CN101486625A CN 101486625 A CN101486625 A CN 101486625A CN A2009100091230 A CNA2009100091230 A CN A2009100091230A CN 200910009123 A CN200910009123 A CN 200910009123A CN 101486625 A CN101486625 A CN 101486625A
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Abstract
The invention provides a fractionation technique for the cracking gas obtained through the oxidation thermal decomposition of gaseous hydrocarbon and used for preparing acetylene. The cracking gas obtained through the oxidation thermal decomposition of gaseous hydrocarbon and used for preparing acetylene first goes through an oil washing tower to remove higher alkyne, C3 hydrocarbon and carbon black, and is pressurized to 0.4MPa to 1.5MPa through a compressor and deoiled through an activated carbon adsorption tower, thus dissolving acetylene and a few other indissoluble components through an absorbed solvent in the adsorption tower; the rest gases go in an ethylene separation tower to recycle concentrated ethylene products and tail gas is taken as synthesis gas; after the solvent dissolving acetylene and a few other indissoluble components enters a flashing tower to remove the indissoluble components, crude acetylene gas is obtained through the separation of an acetylene desorption tower; the indissoluble components are cycled before returning to the compressor and pure acetylene products are obtained after the crude acetylene gas is refined in a carbon dioxide tower; the wash oil saturated with higher alkyne, C3 hydrocarbon and carbon black goes back to normal pressure, flows to a wash oil purifying tower and higher alkyne and C3 hydrocarbon are obtained at the top of the tower and return to serve as gaseous hydrocarbon raw material.
Description
One, technical field
The present invention relates to the splitting gas fractional separation technology of hydrocarbon gas oxidative pyrolysis system acetylene, it belongs to petrochemical industry.
Two, background technology
It is the main acetylene production process except that calcium carbide route at present that the hydrocarbon gas oxidative pyrolysis that Sweet natural gas, coal-seam gas, oil refinery dry gas, associated gas etc. are rich in methane is produced acetylene, the raw natural gas and the oxygen that are preheating to 600-650 ℃ exactly enter multitube burner plate partial oxidation reactor, under 1500 ℃, methane cracking makes the rare acetylene about 8%, carries dense 99% the acetylene finished product that makes with N-Methyl pyrrolidone again.The splitting gas of hydrocarbon gas oxidative pyrolysis system acetylene also contains hydrogen, methane, ethene, carbon monoxide, acetylene homologue, ethane, propylene, propane etc. except that acetylene.Along with the difference of quench liquid, each component concentration of the splitting gas of hydrocarbon gas oxidative pyrolysis has nothing in common with each other.Oil phase is done the chilling agent for water, and energy consumption is low, except that acetylene, goes back a large amount of ethene of by-product.
Contain acetylene the existing separation method of splitting gas be fractional condensation method, fractionating process, cryogenic rectification method, absorption process and absorption method etc., separate acetylene but industrialized separation method is an absorption process.But existing separation method is failed to produce from the hydrocarbon gas oxidative pyrolysis integral body and the comprehensive utilization of each main ingredient of acetylene unit and is considered, under pressurized state, reclaimed acetylene, ethene and synthetic gas (being collectively referred to as of hydrogen and carbon monoxide) are used as low value-added fuel, cause the acetylene cost higher, a large amount of main group of useful wind are not wasted.
Three, summary of the invention
Purpose of the present invention provides the splitting gas fractional separation that the invention provides hydrocarbon gas oxidative pyrolysis system acetylene technology with regard to being to avoid the weak point of above-mentioned technology, the reaction gas of hydrocarbon gas oxidative pyrolysis system acetylene removes senior alkynes, carbon three hydrocarbon and carbon black by oil scrubber earlier, compressed machine is pressurized to 0.4-1.5MPa, again after the activated carbon adsorber de-oiling, by be absorbed dissolution with solvents in acetylene absorption tower acetylene and a small amount of other indissoluble components; The ethylene separation tower that enters residual gas reclaims dense ethylene product, and tail gas is as synthetic gas; After the solvent that has dissolved acetylene and a small amount of other components enters flashing tower and removes the indissoluble component, separate to obtain thick acetylene gas through acetylene stripper; The indissoluble component circulates before returning compressor, and thick acetylene gas obtains pure acetylene product after the decarbonation tower is refining; Be throttled to normal pressure by senior alkynes, carbon three hydrocarbon and the saturated washing oil of carbon black and enter the washing oil scavenging tower, cat head obtains senior alkynes and carbon three hydrocarbon return as gaseous hydrocarbon feedstock.
Lyosorption is methyl alcohol, methyl-2-pyrrolidone, dimethyl formamide, ammonia, acetone or water, and preferred solvent is a methyl alcohol.
Ethylene separation tower is that solid phase transformation complexing absorption, liquid complexing absorb or suspension bed complexed absorption tower, and the optimal ethylene knockout tower is a suspension bed complexed absorption tower.
The decarbonation tower is hydramine absorption tower or soda-wash tower, and preferred decarbonation tower is the hydramine absorption tower.
Four, description of drawings
Accompanying drawing 1 is the process flow diagram of invention.
The drawing of accompanying drawing is established bright as follows:
1, splitting gas inlet 2, oil scrubber 3, washing oil scavenging tower 4, senior alkynes and carbon three hydrocarbon outlet 5, compressor 6, activated carbon adsorber 7, acetylene absorption tower 8, flashing tower 9, acetylene stripper 10, decarbonation tower 11, acetylene outlet 12, carbonic acid gas outlet 13, ethylene separation tower 14, ethene outlet 15, syngas outlet
Below in conjunction with drawings and Examples in detail process characteristic of the present invention is described in detail.
Five, embodiment
The present invention will be described in detail below in conjunction with accompanying drawing: the splitting gas of hydrocarbon gas oxidative pyrolysis system acetylene enters oil scrubber (2) by splitting gas inlet (1) earlier and removes senior alkynes, carbon three hydrocarbon and carbon black, compressed machine (5) is pressurized to 0.4-1.5MPa, again after activated carbon adsorber (6) de-oiling, by lining, acetylene absorption tower (7) be absorbed dissolution with solvents acetylene and a small amount of other indissoluble components; Residual gas enters ethylene separation tower (13) and reclaims dense ethylene product from ethene outlet (14), removes synthesizing methanol from syngas outlet (15) tail gas discharged as synthetic gas; After the solvent that has dissolved acetylene and a small amount of other components enters flashing tower (8) and removes the indissoluble component, separate to obtain thick acetylene gas through acetylene stripper (9); The indissoluble component is returned the preceding circulation of compressor (5), and thick acetylene gas obtains pure acetylene product from acetylene outlet (11) after decarbonation tower (10) is refining, reclaims the raw material of carbonic acid gas as synthesizing methanol from carbonic acid gas outlet (12); Be throttled to normal pressure by senior alkynes, carbon three hydrocarbon and the saturated washing oil of carbon black and enter washing oil scavenging tower (3), from the senior alkynes of cat head with carbon three hydrocarbon outlets (4) obtain senior alkynes and C2 hydrocarbon returns as gaseous hydrocarbon feedstock, loop back oil scrubber (2) at the bottom of the tower behind the separating of oil carbon black and use.
Lyosorption is methyl alcohol, methyl-2-pyrrolidone, dimethyl formamide, ammonia, acetone or water, and preferred solvent is a methyl alcohol.
Ethylene separation tower (13) is that solid phase transformation complexing absorption, liquid complexing absorb or suspension bed complexed absorption tower, and the optimal ethylene knockout tower is a suspension bed complexed absorption tower.
Decarbonation tower (10) is hydramine absorption tower or soda-wash tower, and preferred decarbonation tower is the hydramine absorption tower.
The reaction gas classification separating technology of gaseous hydrocarbon oxidative pyrolysis of the present invention acetylene processed has following outstanding advantage: (1) branch fraction From, having obtained simultaneously acetylene, ethene, synthesis gas and four kinds of products of carbon black, no discarded object is discharged; (2) technological process and energy profit With rationally, be easy to extensive and suitability for industrialized production.
Claims (4)
1. the splitting gas fractional separation technology of hydrocarbon gas oxidative pyrolysis system acetylene, its technical characterictic is that the reaction gas of hydrocarbon gas oxidative pyrolysis system acetylene removes senior alkynes, carbon three hydrocarbon and carbon black by oil scrubber earlier, compressed machine is pressurized to 0.4-1.5MPa, again after the activated carbon adsorber de-oiling, by be absorbed dissolution with solvents in acetylene absorption tower acetylene and a small amount of other indissoluble components; The ethylene separation tower that enters residual gas reclaims dense ethylene product, and tail gas is as synthetic gas; After the solvent that has dissolved acetylene and a small amount of other components enters flashing tower and removes the indissoluble component, separate to obtain thick acetylene gas through acetylene stripper; The indissoluble component circulates before returning compressor, and thick acetylene gas obtains pure acetylene product after the decarbonation tower is refining; Be throttled to normal pressure by senior alkynes, carbon three hydrocarbon and the saturated washing oil of carbon black and enter the washing oil scavenging tower, cat head obtains senior alkynes and carbon three hydrocarbon return as gaseous hydrocarbon feedstock.
2. according to the splitting gas fractional separation technology of the hydrocarbon gas oxidative pyrolysis system acetylene that claim 1 provided, it is characterized in that lyosorption is methyl alcohol, methyl-2-pyrrolidone, dimethyl formamide, ammonia, acetone or water, preferred solvent is a methyl alcohol.
3. according to the splitting gas fractional separation technology of the hydrocarbon gas oxidative pyrolysis system acetylene that claim 1 provided, it is characterized in that ethylene separation tower is that solid phase transformation complexing absorption, liquid complexing absorb or suspension bed complexed absorption tower, the optimal ethylene knockout tower is a suspension bed complexed absorption tower.
4. according to the splitting gas fractional separation technology of the hydrocarbon gas oxidative pyrolysis system acetylene that claim 1 provided, it is characterized in that the decarbonation tower is hydramine absorption tower or soda-wash tower, preferred decarbonation tower is the hydramine absorption tower.
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| Application Number | Priority Date | Filing Date | Title |
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| CNA2009100091230A CN101486625A (en) | 2009-02-19 | 2009-02-19 | Fractionation process for cracking gas from oxidation pyrolysis of gaseous hydrocarbon |
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| CNA2009100091230A CN101486625A (en) | 2009-02-19 | 2009-02-19 | Fractionation process for cracking gas from oxidation pyrolysis of gaseous hydrocarbon |
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Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101942231A (en) * | 2010-08-30 | 2011-01-12 | 江门市三七电池实业有限公司 | Method for preparing acetylene black applied in battery production |
| CN102675028A (en) * | 2012-05-07 | 2012-09-19 | 浙江大学 | Separating preparation method of acetylene by absorbing pyrolysis gas with ionic liquid |
| CN102701896A (en) * | 2012-06-06 | 2012-10-03 | 西南石油大学 | Composite solvent for purifying acetylene and purification method thereof |
| CN103423969A (en) * | 2013-08-30 | 2013-12-04 | 北京麦科直通石化工程设计有限公司 | Method for optimizing ethylene device compression area and reducing outlet pressure of cracking furnace |
| CN105273758A (en) * | 2014-07-25 | 2016-01-27 | 中国石油化工股份有限公司 | Method for separating refinery dry gas by DMF absorption |
| CN105693452A (en) * | 2016-03-31 | 2016-06-22 | 北京神雾环境能源科技集团股份有限公司 | Purifying system and method for acetylene preparation from natural gas |
| CN106422669A (en) * | 2016-08-29 | 2017-02-22 | 查都（上海）科技有限公司 | Method and system for concentrating and recovering acetylene tail gas |
| CN105273757B (en) * | 2014-07-25 | 2017-06-30 | 中国石油化工股份有限公司 | A kind of method of NMP absorption and separations oil refinery dry gas |
| CN108218655A (en) * | 2016-12-21 | 2018-06-29 | 中国石化集团四川维尼纶厂 | The method that gas by partial oxidation of natural acetylene by-product higher alkyne recycles |
| CN108218659A (en) * | 2016-12-21 | 2018-06-29 | 中国石化集团四川维尼纶厂 | Rich advanced alkynes solvent reclamation utilizes method in gas by partial oxidation of natural acetylene technique |
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2009
- 2009-02-19 CN CNA2009100091230A patent/CN101486625A/en active Pending
Cited By (15)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101942231A (en) * | 2010-08-30 | 2011-01-12 | 江门市三七电池实业有限公司 | Method for preparing acetylene black applied in battery production |
| CN102675028A (en) * | 2012-05-07 | 2012-09-19 | 浙江大学 | Separating preparation method of acetylene by absorbing pyrolysis gas with ionic liquid |
| CN102675028B (en) * | 2012-05-07 | 2014-06-04 | 浙江大学 | Separating preparation method of acetylene by absorbing pyrolysis gas with ionic liquid |
| CN102701896A (en) * | 2012-06-06 | 2012-10-03 | 西南石油大学 | Composite solvent for purifying acetylene and purification method thereof |
| CN102701896B (en) * | 2012-06-06 | 2014-06-25 | 西南石油大学 | Composite solvent for purifying acetylene and purification method thereof |
| CN103423969A (en) * | 2013-08-30 | 2013-12-04 | 北京麦科直通石化工程设计有限公司 | Method for optimizing ethylene device compression area and reducing outlet pressure of cracking furnace |
| CN105273758A (en) * | 2014-07-25 | 2016-01-27 | 中国石油化工股份有限公司 | Method for separating refinery dry gas by DMF absorption |
| CN105273758B (en) * | 2014-07-25 | 2017-06-30 | 中国石油化工股份有限公司 | A kind of method of DMF absorption and separations oil refinery dry gas |
| CN105273757B (en) * | 2014-07-25 | 2017-06-30 | 中国石油化工股份有限公司 | A kind of method of NMP absorption and separations oil refinery dry gas |
| CN105693452A (en) * | 2016-03-31 | 2016-06-22 | 北京神雾环境能源科技集团股份有限公司 | Purifying system and method for acetylene preparation from natural gas |
| CN105693452B (en) * | 2016-03-31 | 2017-11-14 | 北京华福工程有限公司 | A kind of cleaning system and method for natural gas acetylene |
| CN106422669A (en) * | 2016-08-29 | 2017-02-22 | 查都（上海）科技有限公司 | Method and system for concentrating and recovering acetylene tail gas |
| CN108218655A (en) * | 2016-12-21 | 2018-06-29 | 中国石化集团四川维尼纶厂 | The method that gas by partial oxidation of natural acetylene by-product higher alkyne recycles |
| CN108218659A (en) * | 2016-12-21 | 2018-06-29 | 中国石化集团四川维尼纶厂 | Rich advanced alkynes solvent reclamation utilizes method in gas by partial oxidation of natural acetylene technique |
| CN108218655B (en) * | 2016-12-21 | 2021-03-19 | 中国石化集团四川维尼纶厂 | Method for recycling advanced alkyne as byproduct in preparation of acetylene by partial oxidation of natural gas |
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Application publication date: 20090722 |